CA2845926A1 - A two-stage gas washing method applying sulfide precipitation and alkaline absorption - Google Patents

Abstract

The present description is related to the field of hydrocarbon production by gasification of carbonaceous material. It provides a two-stage gas washing method as a part of gas refining. More specifically it discloses a method for hydrogen sulfide and carbon dioxide removal from synthesis gas produced by gasification. It introduces a use of a novel combination of two chemical wash approaches for this application. As a specific application, this process is utilized as a part of biomass to liquid (BTL) process.

Description

A two-stage gas washing method applying sulfide precipitation and alkaline absorption Technical field The present description is related to the field of hydrocarbon production by gasification of carbonaceous material. It provides a two-stage gas washing method as a part of syngas refining process. More specifically it discloses a method for hydrogen sulfide and carbon dioxide removal from synthesis gas produced by gasification. It introduces a use of novel combinations of wash approaches for this application involving absorption by chemical reactions. As a specific application, this process is utilized as a part of biomass to liquid (BTL) process.
Background The gasification of carbonaceous material produces primarily carbon monoxide and hydrogen, mixture known as syngas or synthesis gas. Also carbon dioxide, water and various hydrocarbons are abundant side products in the gasification product. Depending on the source and composition of the carbonaceous raw material and gasification conditions, the levels of side products and derivatives typically present as impurities vary influencing the refining strategies.
During gasification, the sulfur components originated from biomass are mainly converted to hydrogen sulfide (H2S) and carbonyl sulfide (COS). In comparison to coal gasification, gasifying biomass raw material produces very low levels of sulfidic, relatively low levels of nitric and low levels of ashes impurities. The level of carbon dioxide is typically higher than in coal gasification. These impurity levels are still harmful for further chemical processing and the gas must be purified. The decrease of hydrogen sulfide concentration is compulsory for the functioning of the catalysts later in the refining of the syngas. On the other hand, the carbon dioxide's role in the further reactions is basically as an inert. The reason for removing CO2 relates to optimizing the streams and decreasing volumes of recycle flows and equipment. The strategies known from coal gasification are not readily applicable.
Together carbon dioxide, hydrogen sulfide and carbonyl sulfide are referred to as acid gas since they dissolve in water forming acids. One of the most common means for gas purification is absorption, which has been used for acid gas removal from natural and synthesis gases. When purifying biomass originated synthesis gas, absorption with a liquid solvent has shown to be more efficient than solid absorption. For physical absorption, organic solvents at cold temperatures and high pressure are common. Roughly, the higher the pressure, the colder the temperature and higher the purity of the absorbent, the better is the washing effect. For chemical absorption, solutions of arsenic salts, various amines and carbonates are known. Generally, the absorbent is regenerated by rising the temperature and/or releasing the pressure.
Prior art discloses effective absorbents for removing acid gas using e.g.
methanol. Methanol requires low temperatures to be efficient and to avoid absorbent loss. A very well-known commercial process using methanol is acid gas removal process marketed under trade name Rectisol . The Rectisol acid gas removal process does not require hydrolysis of COS to H2S
and can reduce sulfur component contents to relatively low levels in syngas.
Methanol has a high affinity for hydrocarbons as well as for acid gas. It also exhibits capabilities to remove not only sulfur components and CO2 but also many relevant trace components (carbonyles, HCN), which makes Rectisol wash a useful process. The syngas is then reheated to about 350 C and passed through a fixed bed of sorbent for sulfur components, such as a ZnO
guard bed, to further reduce the sulfur component contents in the syngas.
Large temperature differences between process phases consume a lot of energy and makes processing expensive.
In prior art, document EP 2223889 discloses a device providing further development of the multistage methanol wash as a part of Integrated Gasification Combined Cycle, IGCC. With the device disclosed, as a multistage process, this version of Rectisol process removes also CO2 from the gas. As a process related to power production, the purity requirements are, however, different from those applied in chemical or fuel production wherein higher purity is demanded.
Another document of prior art, US 2010163803, discloses a process for the production of gas products from a raw synthesis gas that is obtained by gasification of carbon and/or heavy oil.
Origin of the gas gives it a characteristic component profile. The process description discloses how both the shifted and the unshifted gas streams are purified of sulfur components and CO2 in sour gas washing, more specifically a cryogenic methanol washing.
An apparatus suitable for the process is disclosed as well. Sulfur components and CO2 are removed together, the washes providing no separation of these components.
In addition to physical absorption described above, chemical absorption is known in the art.
Gas containing large volumes of hydrogen sulfide can be freed from said hydrogen sulfide by first conducting the gas stream into aqueous solutions containing copper ions in water for absorbing the hydrogen sulfide and then oxidizing the copper sulfide thus formed with air or oxygen gas to produce elemental sulfur. Prior art document DE 2304497 discloses an aqueous absorption medium which contains rather high concentrations of copper ions (28.9

2 g Cu in 1400 ml water), and absorption of the hydrogen sulfide carried out by bubbling the gas into the aqueous medium.
Another document representing prior art, EP0986432 B1, discloses a method for selective hydrogen sulfide removal from gases comprising both H2S and CO2. When these components were present in the gas in CO2to H2S ratio of 2:1, the method removed 99 % of the H2S selectively. However, when said ratio was 200:1, the H25 removal was 95 %.
An old prior art document, U52889197 discloses a two-step gas washing method consisting of two alkaline washes. Both washes are performed with alkali, ammonium is specifically mentioned, and an inorganic salt. The aim is to recover the sulfur component from the wash solution as a sulfate suitable for use as a fertilizer. In column 3, lines 30-31 indicate that after these two alkaline washes, an acidic washing is required. The document discloses no experimental proof on the effectiveness or results obtainable by said method.
There still is a need for an alternative method for removal of sulfur components and carbon dioxide from syngas obtainable by gasification of carbonaceous material, especially when gasifying biomass. Further, there is a need to remove sulfur components and carbon dioxide from the syngas in an energy efficient way. There also is a need for an effective combined sulfur component and carbon dioxide removal. Yet, there is constant need for simplification, increase of the effectiveness and identification of possibilities for synergism of the overall BTL process.
Summary of the invention The present inventors have surprisingly found that a washing method comprising two different chemical absorption steps provides high purity product with lower energy consumption than prior art methods. As the first aspect, a method for washing hydrogen sulfide and carbon dioxide from a gas obtainable by gasification of carbonaceous biomass is provided, comprising a. contacting said gas with a first absorbent solution comprising transition metal ions, said transition metals selected from copper, zinc, iron and cobalt and mixtures thereof, in acidic aqueous solution;
b. binding sulfide ions to said first absorbent solution;
c. recovering the gas from step b;
d. contacting recovered gas from step c with a second absorbent solution comprising an alkaline absorbent:

3 e. binding carbon dioxide to said second absorbent solution:
f. recovering the washed gas from step e.
This method and embodiments thereof provide advantages. One advantage provided by this method is related to process design. When applying two chemical absorption steps, the need for thermal conditioning and heat exchange equipment, especially for cooling, is significantly reduced compared to processes using physical absorption, e.g. methanol washes.
Moreover, the energy consumption is smaller. The two-step washing arrangement is necessary because of high levels of both H25 and 002, but surprisingly the H25 removal in the first absorption step affects the second absorption by moderating the requirements for absorption conditions. As the present method is especially suitable for washing biomass derived syngas, the wash combination, especially at given sequence provides efficient treatment for gas having high CO2 and H25 mole concentrations. This method has proven to produce washed gas having a H25 level of less than 20 ppb, and even lower levels, less than 1 ppb.
As the second aspect, when used as a part of a biomass to liquid process, the washing method is applied among the other process steps providing an improved method for producing hydrocarbons or derivatives thereof. The method then comprises the steps:
i.
gasifying the biomass raw material in the presence of oxygen and/or steam to produce a gas comprising carbon monoxide, carbon dioxide, hydrogen, water and hydrocarbons;
ii. optionally a tar reforming step iii. optionally removing tar components e.g. naphthalene from the gas;
iv. optionally adjusting the hydrogen to carbon monoxide ratio;
v. washing according to claim 1;
vi. converting in a synthesis reactor at least a significant part of the carbon monoxide and hydrogen contained in the gas into a product selected from hydrocarbon composition and derivatives thereof; and vii. recovering the hydrocarbons or derivatives thereof as product.
When the synthesis of step vi is Fischer-Tropsch (FT) synthesis, the wash protocol of step v reduces the levels of acid gases in the feed of FT synthesis process to levels as low as 20 ppb meeting requirements for FT catalysts, and the level of CO2 is low enough to prevent accumulation thereof in the process.

4 Brief description of the figures Figure 1 illustrates an experiment (Example 1) comprising contacting the gas with a first absorbent solution, here aqueous CuSO4 solution, binding sulfur components from gas thereto and recovery of gas according to steps a, b and c of claim 1. In the figure, a ratio of H2S mole flow in the wash bottle outlet/H2S mole flow in the wash bottle inlet as a function of time [h:min] is disclosed. The experiment was started at 9:33 and last point measured 15:11.
Figure 2 illustrates another experiment (Example 2) similar to that of Figure 1. The experiment was started at 9:53 and last point measured 15:16.
Figure 3 illustrates yet another experiment (Example 3) similar to that of Figure 1. The experiment was started at 10:43 and last point measured 13:22.
Figure 4 discloses a simple flow diagram of an embodiment of the method of the present invention for H25 and CO2 removal by a two-stage process.
Detailed description of the invention Herein is provided a novel method for washing of hydrogen sulfide (H25) and carbon dioxide (CO2) from a gas obtainable by gasification of carbonaceous biomass.
Characteristic for this method is that it involves two consequent washes, both based on chemical absorption but involving different reactants and reaction strategies. The first wash comprises a. contacting said gas with a first absorbent solution comprising transition metal ions, said transition metals selected from copper, zinc, iron and cobalt and mixtures thereof, in acidic aqueous solution;
b. binding sulfide ions to said first absorbent solution;
c. recovering the gas from step b.
The first wash removes selectively hydrogen sulfide from the gas. The removal efficiency is high. At least 90 %, preferably at least 95 % of the hydrogen sulfide present in the feed can be removed in this step.
The second wash comprises d. contacting recovered gas from step c with a second absorbent solution comprising an alkaline absorbent;
e. binding carbon dioxide to said second absorbent solution;

5 f. recovering the washed gas from step e.
The second wash principally removes carbon dioxide. As the concentration of sulfide ions has already been considerably diminished in the first wash step, the absorbing capacity of the second absorbent, thus alkaline absorbent can be utilized mainly for the carbon dioxide removal. The inventors have found that the hydrogen sulfide concentration is further lowered in the second wash providing recovered gas of such a high purity, that in some cases guard beds removing H2S prior to synthesis reactions can be omitted.
When applying the method of the present invention, the selection of the conditions for the second wash can be less stringent than when applying corresponding alkaline absorbent detached. Preferably the second absorbent solution is applied as an aqueous amine wash, carbonate wash, carbonate precipitation or a combination thereof. The temperature, pressure, recycling etc. need not to be pushed to extremes to obtain desired purity levels.
Especially notable is the temperature with which high purity was acquired also experimentally.
Yet another benefit of the present invention is that when applying sequential removal of H2S
first and CO2 after that, these unit processes are essentially independent from each other.
Especially, the second wash step can be steered to purity level required by the following processing without compromising the ultraclean character of the first absorption step. Thus, independent control of the removal of acid gases is possible through the present method.
As used herein, "absorbent solution" refers to a wash liquid used for washing the gas. For processing purposes, as fresh, it is preferably a true solution, thus all components are dissolved in the solvent, here aqueous solutions. A person skilled in the art understands, that when used, especially when there has been a chemical reaction involved, said absorbent solution may contain solids or precipitates.
With "binding a gas (hydrogen sulfide or carbon dioxide) to an absorbent solution" is meant basically absorption of said gas to said solution. It includes all phases of absorption, material transfer from gas to gas-solvent interface, shift from gas to liquid phase, and in the case of a chemical absorbent the chemical reaction in question.
The two-stage method removes preferably at least 99 %, preferably at least 99.9 % of the H2S present in the feed gas. Of the carbon dioxide, the removal is at least 90 %, preferably at least 95 % of the CO2 present in the feed gas.
When describing the process, measurements, and results, the proportions given are percentages of the total gas volume of the dry gas unless otherwise stated.

6 An illustration of the method is given in Figure 4, which discloses a simple flow sheet of an embodiment of the method of the present invention for H2S and CO2 removal by a two-stage process. In said figure 4, the raw syngas is fed to an optional hydrolysis reactor, which converts HCN and COS, followed by an optional water wash reactor, from the outlet of which aqueous HCI and NH3 are removed. The essence of the invention lies within the next two reactors. The first of these is a reactor named in the figure 4 as CuS
precipitation unit. In said reactor, the gas is contacted with dilute aqueous CuSO4 solution. With sulfides originating from gaseous hydrogen sulfide, copper forms CuS, which is practically insoluble in water and precipitates out of the solution.
Gas thus recovered is next led to alkaline absorption unit to remove CO2.
Aqueous alkaline absorbents have good capacity to remove acid gases, but as major part of gaseous hydrogen sulfide has already been removed in the preceding step, the unit is designed for CO2 removal only.
According to the embodiment described in Figure 4, the gas is fed to the absorber from a gas scrubber. The first absorption step in acidic aqueous solution can preferably be performed at the same temperature as said scrubbing, as well as the second wash with alkaline absorbent solution.
Optionally a guard bed (Figure 4) or multiple guard beds can be added downstream of the units, for safety and in case of abnormal situations.
The combination of first and second absorbents according to claim 1 has surprisingly proven to allow separate recovery of CO2 and H25 providing savings in energy consumption in comparison to one step methanol wash when removing both H25 and CO2. When judged against methanol wash requiring cold conditions (typically temperatures below 0 C), the present method provides substantial benefit with regard to operating temperature and energy consumption and cooling equipment requisites thereof.
1. Feed characteristics When refining syngas obtainable from gasification of biomass the acid gases consist mainly of H25, CO2 and COS. As an example of a typical composition, the gas composition fed to acid gas wash comprises as main components (calculated of the dry gas) from 20 to 40 vol-% H2, from 10 to 30 vol-% of CO, and as acid gas impurities from 50 to 400 ppm H25, from 20 to 40 vol-`)/0 CO2 and 5 to 50 ppm COS and other traces.
Special characteristics for refining gas originated from biomass are the high CO2 and H25 concentrations. If there is a need to recover these components separately, the prior art

7

8 PCT/F12012/050816 references suggest using physical absorption, as chemical absorbents tend to remove CO2 and H25 simultaneously.
2. Transition metal ions In the method for washing hydrogen sulfide and carbon dioxide from a gas obtainable by gasification of carbonaceous biomass, the first step of this method comprises first contacting said gas with a first absorbent solution comprising transition metal ions in acidic aqueous solution.
This step is efficient for H25 removal. The present inventors found that in acidic aqueous solutions transition metal ions, for example Cu2+ ions, react fast with H25 in liquid at even very small metal ion concentrations. The results were evidenced in patent application EP11153704 disclosing a method of purifying gasification gas (syngas) by absorbing impurities of syngas in a liquid absorption medium containing metal ions capable of binding sulfide ions into solid sulfides which have low solubility in water and aqueous solutions. Thus, said metal ions, preferably predominantly bivalent transition metal ions, have effect of binding sulfides, present as H25 in the gas phase, from gas to said first absorbent solution. When reacted with this solution, the gas is recovered for further processing.
Another document, EP0986432 B1, discusses the theory, especially the precipitation characteristics exhaustively from paragraph 27 to paragraph 43.
However, now the inventors have further developed the idea and proved that when transition metal ion absorption for H25 removal, as the first wash, is combined with an alkaline absorption for 002 removal, said absorptions together provide unexpected synergism.
This first step is carried out by contacting the gas with the first absorbent solution, thus an acidic aqueous wash solution containing transition metal ions capable of binding to sulfide ions of the sulfide compounds present in the gas. The concentration of the transition metal cations is small, for example the aqueous solution has a concentration in respect of the transition metal ions of about 0.00001 to 0.01 M. A significant portion of the sulfide impurities present and contained in the gas can be converted into transition metal sulfides. The sulfides thus formed are preferably precipitated from the wash solution whereby the sulfide impurities are removed from the gas. The purified gas so obtained is recovered from the aqueous solution.
The metal ions, i.e. cations, of the wash solution are derived from transition metals selected from copper, zinc, iron and cobalt and mixtures thereof. Preferably the wash solution comprises bivalent metal cations (Me2+) of copper (Cu2+), zinc (Zn2+) or iron (Fe2+) or mixtures thereof, because these cations react with sulfides (S2-) forming salts with very low solubility in water. In practice, most suitable salts used as metal cation sources comprise traces of other metal derivatives as well, e.g. commercial CuSO4 salt comprises also some monovalent copper, as Cu2SO4. Copper has proven cost efficient and shown successful in experimental studies, especially when added as CuSO4.
The transition metal ions are obtained from water soluble metal salts by dissolving said salts in water. In one embodiment, the aqueous solution is prepared by dissolving about 1 to 10,000 parts, preferably about 50 to 5000 parts by weight of a metal salt into 1,000,000 parts by weight of water (ppmw).
When applied to H25 removal from syngas obtainable from biomass gasification, typically the concentration of the metal ion compound of the wash solution can be lower than about 1000 ppmw, preferably lower than 100 ppmw, calculated from the weight of the absorption liquid.
This allows for very effective and profitable integrated process concept for removal of H25 and other impurities mentioned above from syngas.
The concentration of Me2+ ions in the aqueous wash solution is typically about 0.00005 M to 0.005 M per litre, preferably about 0.0001 to 0.001 M.
The aqueous wash solution is acidic or weakly acidic; preferably it has a pH
of about 1 to 6.5, in particular about 1 to 5. The pH will vary within the indicated range depending on the selection of the metal cations. For example, in the embodiment in which metal cation source is Cu504, the aqueous solution has pH of at least about 3, preferably pH from 4 to 5.
Generally, the gas is contacted with the wash solution at a temperature from 10 to 80 C and at a pressure from 1 to 50 bar (absolute pressure). Thus, the washing can be carried out at ambient temperature and pressure (20 to 25 C and 1 bar(a)), although it is equally possible to work the present technology at lower temperatures (10 to <20 C) and at elevated temperatures (>25 to 80 C). The pressure can be in excess of 1 bar(a), for example about 1.5 to 50 bar(a). As both the first absorption step and second absorption step are based on chemical absorption, the need for cooling and thus energy consumption are not as high as it would be for physical absorption.
Typically, the syngas obtained from gasification is recovered at higher temperature than indicated in the preceding. Therefore, in one embodiment, the gasification gas is cooled to a temperature within the above indicated range (from 10 to 80 C) before being contacted with the washing liquid. When the temperature is higher than 80 C the reaction is fast, but the precipitate is formed as very fine particles which are difficult to recover from the wash liquid.
If the temperature is below 10 C, the need for cooling raises the operating costs. It is

9 possible to recover some of the heat contained in the gasification gas by contacting it with a cooling media, for example with cooling water, in a heat exchanger.
Under these conditions, also acidic compounds, such as hydrogen chloride, may be absorbed. Further, the aqueous, metal ions containing solution can be applied in acidic form.
Thus, it will be capable of absorbing further impurities, such as ammonia (NH3) and hydrogen chloride (HCI) as well as other alkaline and acidic impurities. For the overall process, this is a further advantage.
The molar ratio of metal cations to sulfide compounds of the gas to be purified (i.e. Me2+/S2-ratio of the feed) is typically in excess of 1, preferably from about 1.4 to about 6. Surprisingly, the use of metal ions is efficient and no great excess is needed, because the reaction proceeds nearly irreversibly as precipitated MeS exits the solution.
3. Process equipment Technically, said contacting gas with a first absorbent solution comprising transition metal ions in acidic aqueous solution may be implemented in tray or packed column and/or applied by spraying or atomizing. In a first preferred embodiment, the contacting of the syngas with the absorption medium takes place by spraying or atomizing the absorption medium into the gas. Preferably, the contacting of the syngas with the absorption medium takes place in the interface between the gas and droplets of the absorption medium. In a second preferred embodiment, the gas to be purified is bubbled into a stirred tank containing the absorption solution. In a third embodiment, absorption towers with plates and/or packing can be used in a counter-current operation. The detailed equipment type depends on the concentration of the metal ions in the solution and the amount and impurity content of the gas.
One way of performing the chemical absorption process is to use chemical spray absorption concept combined with sieve tray(s) above the spray chamber section(s) as described and shown in Figure 6 of application EP11153704.
Thus, in one particular embodiment based on the spray chamber approach, the wash solution is contacted with the gas in a spray chamber having an essentially vertical central axis, said gas being fed into the spray chamber from the bottom or from the top and withdrawn from the opposite end so as to advance in the direction of the central axis of the spray chamber. The wash solution is fed through spray nozzles arranged in at least two spray zones arranged in series along the central axis at different heights in the spray chamber. The gas is fed into a spray chamber, for example of the preceding type, via gas distributors arranged below the lowest spray zone, and the metal sulfide is withdrawn from the absorber along with the used wash liquid via an outlet arranged in the bottom part of the chamber.
In an embodiment, wherein regeneration is applied, after the absorption of the sulfides, MeS-crystals and other solids are separated from circulated aqueous wash liquid.
A transition metal ion washing unit can also consist of two aqueous Me2+ wash sections (named following the direction of the gas flow), wherein the first section is operated with an aqueous wash dilute with Me2+-ions and the second section with another aqueous wash rather highly concentrated with Me2+-ions. The necessary amount of Me2+-ions is fed in the form of an aqueous Me2+-solution into the second wash section and circulated.
Synthesis gas from the first wash section will be fed into the second wash section where almost all of H2S in synthesis gas will be removed by counter-current wash.
The purification results using transition metal ions in acidic aqueous washing liquids are very good. The present method is capable of removing a significant portion of the hydrogen sulfide from the gas. At least 98 % by volume, preferably at least 99.5 %, of the hydrogen sulfide is removed from the gas. As a result, in a preferred embodiment, the concentration of hydrogen sulfide of the gas after the first wash step is less than about 100 ppb by volume, in particular less than about 50 ppb by volume. This is further diminished by the second wash step removing mainly carbon dioxide, but reducing the hydrogen sulfide content to less than ppb, preferably less than 10 ppb or even less than 1 ppb.
20 The gas purified in the first absorption provides the feed for a second absorbent solution comprising an alkaline absorbent selected from amines, carbonates and combinations thereof.
4. Alkaline absorption Alkaline washes using aqueous solutions of amine and/or alkaline metal ion compound as such are known in the field of acid gas purification. In general, the reactions between the acid gases, H2S and CO2 are competing against each other for the alkaline reagent.
Therefore, introducing alkaline absorption subsequently to the aqueous transition metal wash, which has already removed H25, provides unexpected advantages for CO2 removal. In said alkaline absorption, alkaline absorbent is selected from amines, carbonates, aqueous CaO solution and combinations thereof.
In the context of the present invention, it is understood, that alkaline absorptions are performed using aqueous solutions comprising an amine or a carbonate or comprising amines, carbonates or mixtures thereof. By definition, said washing solutions, absorbent solutions or washing liquids, especially after use, comprise impurities bound thereto, at least as trace amounts also after the optional regeneration.
Preferably said alkaline absorption, hence the contacting of gas obtained after first wash with a second absorbent solution, takes place at a temperature from 10 to 80 C, preferably from 20 to 40 C for amine washes. This provides a benefit that the process conditions need not to be altered between two chemical absorption steps of the present method.
Another preferable option is that the temperature of the second wash stage can be selected to be compatible with the process step following thereafter.
Amine wash The reaction of amine with H2S is very fast. The rate determining factor in this reaction is therefore the transition of H2S to gas/liquid surface. The reaction of amines with CO2 is slow and is the limiting factor in CO2 absorption. The reactions between amines and COS, CS2 and CO2 consume amines whereby regular purification of the absorbent solution and adding of fresh amine solution is rendered necessary.
Amines are classified as primary, secondary and tertiary amines depending on the status of the nitrogen atom of the amine i.e. how many carbon atoms are bonded to the amine nitrogen. In the context of acid gas absorption, the primary amines show the highest reactivity.
Primary and secondary amines in general show no specificity towards H2S or 002. Therefore selective removal is not feasible using a primary or secondary amine only.
Tertiary amines, though, are suitable for selective H25 or CO2 removal, as they exhibit faster reaction rates towards H25 than 002. In the present invention, the selectivity is provided by the first absorption phase, the transition metal wash, and the selectivity of second wash is not crucial.
Therefore, the restrictions limiting the traditional amine washes are of minor relevance in the method of the present invention. Selection of a suitable amine is more relaxed and can be made based on criteria other than selectivity.
The most commonly used amines in industrial plants are the alkanolamines.
Commercially available are e.g. monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA). Some chemical providers market reagents 2-(methylaminoethanol), 2-aminohexan-1-ol, diisopropanolamine, 2-(2-aminoethoxy)ethanol, methylamine, dimethylamine (DMA) and trimethyamine (TMA) for amine washes. A man skilled in the art is well aware that these reactants can typically be applied together with additives, preferably selected from hydrocarbons substituted with nitrogen, such as piperazine. The additive content can be quite high, but preferably not exceeding 20 mol- /0 of the amine content. One effect obtained by the use of additives is the decrease of the need for recycling.
Typically the amount of the amine in aqueous absorbent solution is from 5 to 30 wt-%, preferably from 5 to 55 wt-%, and most preferably from 20 to 40 wt-% the remainder being mainly water. Too low an amine content lowers the absorption efficiency, whereas too high increases the corrosion of the process equipment. The amine content can also be adjusted to serve the purpose, thus provide the desired CO2 level.
Carbonate wash The absorbent solution for alkaline metal ion containing wash can be formed by dissolving metal ion containing compound in water. The cation does not form precipitates in the conditions of the wash, but reacts with the acid gases. Commercial processes using hot potassium carbonate (K2CO3) are called Catacarb and Benfield. The process may further comprise a catalyst or an additive. The additive increases removal efficiency for H2S, CO2 and COS, and can typically be selected from amines. Preferable process temperature in carbonate wash is higher than for amine washes, from 70 to 120 C, or even up to 200 C in some embodiments, because the increase in temperature increases the absorption respectively. Preferable process pressure is from 10 to 125 bar.
Carbonate precipitation For the CO2 removal, another method available is precipitation with calcium ions. Thus, aqueous alkaline absorbent comprises CaO. According to this embodiment, CaO
powder is mixed and at least partially dissolved in water. Ca(OH)2-water solution is fed into mixed reactor or spray unit for spraying according to routine practice. The pH of this solution is kept alkaline.
In mixed reactor the gas is introduced into the reactor through a sparger and dispersed into small gas bubbles reacting with Ca(OH)2. CO2 is precipitated with calcium ions forming solid CaCO3. Precipitate is removed from the solution and washed gas recovered for further refining.
As an additional benefit in the precipitation process, the alkaline solution also contributes to simultaneous capture of chlorine impurities from the synthesis gas. If the aqueous Ca(OH)2solution is recycled, it is led through an ion exchange resin bed where S- and Cl-ions are removed from the solution according to known practice.

5. Energy consumption The method of the present invention, as defined in claim 1, comprises two chemical absorption steps. In absorption processes, there are three stages determining the energy consumption level. Preferably parameters contributing to low energy consumption are selected.
The first one is the conditioning of the gas (preheating or precooling of the gas) to be washed before feeding to the absorption stage. For chemical absorption the applicable temperature range is much broader and need for thermal conditioning at this stage is typically lower than for physical absorption. In many cases, no conditioning is needed, as the chemical wash can be performed at the temperature of the preceding process step.
As the combination of the two chemical absorption methods according to the present invention is concerned, it is especially beneficial when low temperature waste heat is available, e.g. from adjacent or related processes or process steps. The energy retrievable from such sources is adequate to provide a temperature suitable for these chemical absorption reactions. The energy can be even cost-free.
Herein, according to an embodiment of the invention, both chemical absorption steps can be selected to take place in mutually substantially corresponding conditions.
Preferably both chemical absorption steps take place at the same temperature or at the same pressure or both. In other words, contacting of the gas with the second absorbent solution takes place at substantially the same temperature and/or same pressure as said contacting of the gas with the first absorbent solution. More preferably, both of these conditions, temperature and pressure are substantially the same. This provides advantages for the process design and/or for the operation costs, as units for heat exchange or pressurizing are not needed in-between first and second absorption units.
The next energy intensive phase consists of the absorption stages. Therein, depending on the reagents, conditions and level of purity selected, there can be need for cooling or heating the reactor and/or reagents.
The third point where energy consumption must be considered is the regeneration of the absorbent. In case of chemical absorption methods, this is very relevant aspect for energy consumption, because regeneration of chemical absorbents is energy intensive.
Savings in regeneration energy produce significant benefits for the overall process.

Embodiments of alkaline absorption combinations According to one specific embodiment of the present invention, the CaCO3 precipitation as alkaline wash is applied in a plant, which is connected to a pulp and/or paper mill. The CaCO3 formed in the alkaline wash can be regenerated back to CaO in the lime kiln of the mill exploiting existing facilities. No need for new storages arises, because CaCO3 is a common ingredient in paper and board mills.
As an embodiment of the present invention, after the first absorption step, the amine wash can optionally be followed by another amine wash, carbonate precipitation or carbonate wash. For example, amine wash can be combined with carbonate precipitation, wherein the alkaline cation is selected to form a precipitate which is poorly soluble in water. The precipitate, e.g. CaCO3 can be used in papermaking. Alternatively, the amine wash can be boosted by a carbonate wash, wherein the cation is selected so that no precipitate is formed.
Yet another option is to combine the first absorption step with second absorption, comprising amine wash followed by carbonate wash which is further intensified by carbonate precipitation.
6. Regeneration of the absorbent As an embodiment of the invention, the method can further comprise regeneration of first or second absorbent solution or optionally both.
Depending on the absorbent and the level of purity required, three procedures for regeneration thereof are known to a man skilled in the art. The most simple and cheapest method for regeneration is the flash regeneration, wherein the absorbent pressure is decreased e.g. gradually. The acid gas concentration is determined by the last step, the pressure of which usually is slightly higher than ambient pressure. By employing vacuum in the last step, the acid gas concentration in the absorbent can further be lowered.
When higher purity is required, the regeneration can be performed by stripping the absorbent with an inert gas. In stripping, the absorbent pressure is lowered and thereafter the partial pressures of the gases to be removed are decreased by feeding inert gas to the reactor. A
negative side of this regeneration system is the dilution of the acid gas flow with inert gas used.
Both regeneration methods, flash and stripping, still leave some acid gas to the absorption solvent. For cases, where the level of hydrogen sulfide to be removed is very low, these methods are sufficient. However, for high hydrogen sulfide concentrations regeneration based on solvent boiling e.g. hot regeneration are needed. This provides very high degree of purity for the gas to be washed and additionally high acid gas concentration in the effluent gases. The principle underlying this method is that gas solubility into the absorbent solvent is reduced by rising the temperature. The solvent is heated to its boiling point, whereby the vaporized solvent strips off the impurities. When the vapor is thereafter cooled down and condensed, it can be reused in the absorption. Hot regeneration requires expensive heat exchangers and consumes heat for vaporization of the solvent, which makes it the most expensive of the methods mentioned. However, hot regeneration is often necessary for chemical absorbents as the acid gases are chemically bonded thereto.
Preferably the regenerated absorption solution can be conditioned and returned to the absorption process.
7. Recovery of metal sulfides Furthermore, from the aqueous solution or slurry, the metal sulfides, which have poor solubility to the aqueous media, can be removed by any solid liquid separation process.
Separation of solids is simple and many separation techniques, such as filtration, settling or hydrocyclones, are available. Such a separation is attractive in comparison to prior art methods, wherein the regeneration of the H2S containing absorbent is typically conducted in a regeneration section. From said prior art regeneration section the sour gases separated from absorbent are led to a sulfur plant converting H25 into elemental sulfur (S). Such investments can totally be avoided.
Metal sulfide precipitate can be further treated to separate the metal and sulfur derivative and both consequently recovered. For example, when metal sulfide is CuS, separated solids can be utilized as raw material in copper industry, either for preparation of metallic copper or other copper compounds, and sulfur recovered from that process can be used as raw material for sulfuric acid production, typically integrated to the site.
8. Use of the purified gas After the treatment according to claim 1, purified gas is obtained. The level of H25 in gas recovered from step e is less than 20 ppb, preferably less than 10 ppb, and most preferably less than 1 ppb. The purified gas has several uses. It can be used for producing hydrogen, methanol, ethanol, dimethyl ether or aldehydes optionally by hydroformulation or directly used in engines for producing for example electricity. Also synthetic natural gas (SNG) can be produced from syngas.
According to an embodiment of the present invention, the purified gas can also be used for producing a hydrocarbon composition containing a4-C90 hydrocarbons, optionally after further purification. In particular, the hydrocarbon composition can be produced by a Fischer-Tropsch (FT) process.
As a specific embodiment of an overall process, the acid gas removal can be applied in a process for hydrocarbons or derivatives thereof production from biomass raw material. The method then comprises the steps:
i. gasifying the biomass raw material in the presence of oxygen and/or steam to produce a gas comprising carbon monoxide, carbon dioxide, hydrogen, water and hydrocarbons;
ii. optionally a tar reforming step;
iii. optionally removing tar components e.g. naphthalene from the gas;
iv. optionally adjusting the hydrogen to carbon monoxide ratio;
v. wash according to claim 1;
vi. converting in a synthesis reactor at least a significant part of the carbon monoxide and hydrogen contained in the gas into a product selected from hydrocarbon composition and derivatives thereof; and vii. recovering the hydrocarbon or derivative thereof as the product.
According to a preferable embodiment, steps are taken in said order from i to vii with or without optional steps. Even though wash according to claim 1 is here referred to as wash step v, it is understood to comprise all the features of claim 1 as filed.
The removal of H2S is necessary to protect the synthesis catalysts.
Furthermore, when applying this method for hydrocarbon production using FT synthesis, even though CO2 acts as an inert in the synthesis, it affects the synthesis selectivity guiding towards 05+ products, whereby at least partial removal of CO2 is rendered desirable for the overall process.
Contrarily to the processes disclosed in the prior art documents for coal derived syngas purification, the attention in acid gas removal, when applied for biomass originated gas, is mostly paid to CO2 removal.
Another considerable value in favor of the present process is that high pressure advances both absorption and the subsequent FT synthesis. If the pressure is increased before the absorption or at least before the second wash of the present method, there is no need to alter the pressure after washes. A man skilled in the art apprehends that increasing the pressure in absorption above the level needed for the level required for FT
synthesis is not preferable, though possible. Typically the pressure employed in FT-synthesis is from 20 to 60 bar, preferably from 20 to 30 bar, which practically sets the upper limit to the absorption process.
In an embodiment of this method, use of iron and cobalt as metal ions in the first absorbent solution is advantageous, because they are used in other parts of the overall process, in particular as FT synthesis catalysts. However, copper is the preferred metal ion, particularly as CuSO4.
Optionally, the process can comprise a tar reforming step, e.g. according to patent application Fl 20105201. It discloses a method for purifying the gasification gas from tar-like impurities and ammonia by using catalysts at high temperatures. The pre-catalyst zone comprises a zirconium/noble metal catalyst layers followed by the actual reformer catalyst zone comprising a nickel or another reforming catalyst layer(s). Oxygen or another oxidizer, and optionally steam, can be led to the reforming zone to increase the temperature.
For FT catalytic synthesis, the hydrogen to carbon monoxide molar ratio is preferably from 1.7 to 2.2, advantageously about 2. To adjust the ratio, a man skilled in the art can select between different strategies. Said ratio can be adjusted by a water gas shift (WGS) reaction either as sour gas shift or after appropriate gas sweetening. Another approach is to add hydrogen obtained from elsewhere in the process or from another process to adjust said ratio.
To some extent, COS may be hydrolyzed in the absorption of the present invention.
However, sometimes a separate hydrolysis is needed. According to an embodiment of the above method for hydrocarbon production, step v is preceded by a COS
hydrolysis step.
Said hydrolysis produces H25, which is consequently removed in the first absorption step and CO2 removed in the second absorption step of the wash process of the present invention. This is beneficial in cases where the synthesis gas contains distracting amounts of COS. COS has poor solubility to chemical absorbents, causing difficulties in purification.
In addition, according to one embodiment, it is also beneficial to operate a water scrubber before the wash steps to minimize NH3 and HCI in transition metal precipitation stage. Said NH3 and HCI interfere metal precipitation stage and their removal contributes to purer CuS
precipitate.
The following experiments were conducted to evidence the concept of the present invention.
They should be understood illustrating certain examples of the invention and no limiting by any means.

Experimental part The method of the present invention is a two-stage washing process.
The first phase, absorption using an aqueous solution comprising transition metal ions, was described in the applicant's earlier patent application EP11153704. Examples 1 and 2, apply for the first phase of the present invention as well. In said first phase, the gas to be purified is contacted with a first absorbent solution comprising transition metal ions, said transition metals selected from copper, zinc, iron and cobalt and mixtures thereof, in acidic aqueous solution (in the experiments aqueous CuSO4 solution); hydrogen sulfide is bound to said first absorbent solution and gas recovered.
The combination of first and second absorption phases is studied as a simulation. Said simulation provides data on the stream compositions and process parameters.
Simulation settings and results thus obtained are given as example 3.
1 Example 1. Semibatch absorption tests of H25 removal, using aqueous copper sulfate (Cu504) as a model absorbent of the first absorbent solution.
1.1 Materials and methods The absorption experiments were carried out using a micro reactor equipment for WGS
reaction. Semibatch absorption tests of H25 removal, using aqueous copper sulfate (Cu504)-solution as absorbent, were carried out in a simple 0.5 liter gas-wash bottle with magnetic stirring, placed in the product line of a micro reactor before the online mass spectrometer.
Absorption tests were carried out at room temperature and atmospheric pressure. Total gas feed flow was 12 dm3/h to the WGS reactor. The basic gas feed composition is shown in Table 1.
Table 1. Basic feed composition.
Total flow H20 CO CO2 H2 N2 CH4 litre(NTP)/h vol-% vol-% vol-% vol-% vol-% vol-%
12.0 36 12 22 24 5 1 The impurity components were purchased from AGA as dilute hydrogen mixture gases H25/1-12, COS/H2 and NH3/H2. In the feed, H25 concentration was 500 ppm (vol) in all experiments. In some tests also 85 ppm COS and 800 ppm NH3 were used in the feed.
However, nearly all COS was hydrolyzed already before the absorption bottle as it was not possible to bypass the catalytic reactor, where COS hydrolysis took place as a side reaction of water gas shift reaction.
The product gas was analyzed online using a mass spectrometer (GC-MS but GC
separation not in use). The quantitation limit is dependent on the component, and in these MS
measurements quantitation limit was about 1 ppm.
In absorption experiments carried out in laboratory in bubbled gas wash bottle described above the following test program was carried out as follows:
= The CuSat concentration varied in different experiments from dilute 50 ppm up to 500 ppm. The mass transfer in the bubbled gas wash bottle was enhanced by agitation.
. Absorption rate of H25 in Cu504-water solution was measured at different CuSat concentrations.
= Identification/quantification of crystallized Cu-solid components and particle size distribution of crystallized particles.
1.2 Results The feed rates of different impurity components in synthesis gas entering WGS
reactor in the experiments were:
= Test 1 ¨ CuSat conc. 0.01wt-`)/0, H25 concentration in feed gas 500 ppmv = Test 2 ¨ CuSat conc. 0.01wt-`)/0, H25 concentration in feed gas 500 ppmv, NH3800ppmv, COS 85 ppmv = Test 3 ¨ CuSat conc. 0.0051wt-`)/0, H25 concentration in feed gas 500 ppmv, NH3800ppmv, COS 85 ppmv H25 mole flow in wash bottle outlet / H25 mole flow in wash bottle inlet in different experiments are shown as a function of time in Figures 1-3.
1.3 Conclusions CuSat was capable of removing 500 ppm H25 (mol-frac) completely from feed gas both with 0.01 and 0.005 wt-% aqueous solutions. The product is solid CuS deposit.

= Too high pH resulted in deposition of e.g. metal hydroxides or carbonates in which case no or less hydrogen sulfide was removed. Carbonate formation was also dependent on CO2 partial pressure.
= Too low pH resulted in no deposit formation in which case no hydrogen sulfide was removed (results not shown).
= NH3 in the feed did not influence H2S removal by copper sulfate.
With regard to the results described in the figures 1-3 it should be pointed out that the experimental setup was the following: the bottle of aqueous copper sulphate wash solution was placed after two reactor product coolers but before drum type volumetric gas flow meter.
By opening the valves the gas could be made to flow through the CuSO4 aqueous solution and after that to the GC-MS, and subsequently the gas was conducted to the drum type volumetric gas flow meter for venting. The first point shown graphically is from the point of time immediately before the gas was conducted to the CuSat bottle. At that point of time, precipitation of CuS is not detectable yet. Then, a series of 4 samples was taken within 7 minutes, and after a short break, a new series of 4 samples was taken within 7 minutes etc.
The points in the figures in which the H25 concentration is 0 indicate points where all H25 is removed from the gas. Suddenly after that all the copper is depleted and the concentration increases again.
Some of the tests have contained COS in the feed. Having passed the shift reactor it has in practice been completely hydrolyzed since the feed also contains water:
COS + H20 <---> H25 + CO2 Then, there is more H25 in the feed of the CuSat washing than the amount of H25 fed into the system. This effect could be seen in the analysis in the amount of effluent COS 0-3 ppmv=
2 Example 2. Absorption test for H25 removal from syngas in packed bed absorption column.
Absorption tests for H25 removal from syngas in packed bed absorption column were carried out in a Pilot scale test unit. The absorber performance was tested in a syngas preparation plant in Varkaus, Finland.
Absorber details and data sheets are shown below:
Absorber: = packed bed absorber, packing metal, 2-in or 50 mm, surface area 100 m2/m3, = height: 9 m, diameter 0.1 m.
Feed Gas: = feed rate: 50-60 kg/h = pressure 30 bar, temperature 25 C
= Composition/mol-%: CO 21, CO2 30, H2 31, CH4 3, N2 15, H2S 140 PPM, naphthalene 100 ppm, benzene 1200 ppm and traces NH3 and COS.
Absorbent Feed:
= CuSO4¨water, concentration 0.15 wt-%
= Feed rate was varied, equivalent Cu2+ molar feed ratio to H25 1.5-6 The mol-`)/0 of H25 in effluent gas was measured by on-line hydrogen sulphide gas analyser.
The measured H25 mole fraction in effluent syngas was at minimum 70 ppb at equivalent Cu2+ molar feed ratio to H25 value of 6.
As a result, the correlation between product gas S concentration and stoichiometric Cu/S
ratio in the feed was determined. For stoichiometric ratios from 1 to 5 almost linear correlation was observed, wherein the stoichiometric ratio of 1.5 for Cu/S led to less than 3 ppmv H25 and ratio 5 led to 90 ppbv H25 in the product gas.
3 Example 3, A simulation of the method for washing hydrogen sulfide and carbon dioxide according to the present invention combining a Cu504 wash and an amine wash In this example a two-stage wash according to one embodiment of the invention was simulated. The first step with aqueous Cu504 as absorption solution was simulated with Aspen Plus flow sheeting program with the following process parameters:
= The absorber models are rate-based models realized in Radfrac = The physical property and VLE method of ELECNRTL
= All reactions, except for Cu-reaction, Henry-components, parameters, etc. are set as Aspen Plus defaults and realized through the Electrolyte wizard The second wash step, contacting recovered gas from step c with a second absorbent solution comprising an alkaline absorbent was simulated with ProTreat simulator. This simulator is especially suitable for amine wash simulations.

The results from the simulations are given in two tables. First, table 2 discloses hourly flows of the main components as moles. It gives calculated compositions for feed and treated gas.
From the same simulation data, the operating conditions were calculated as well. The second table (table 3) gives calculated energy consumption values exhibiting the good energy economy of the method according to the present invention in comparison to methanol wash.
Table 2. Two stage wash according to an embodiment of the invention.
Mole flow [kmol/h] Syngas in Syngas out H2S 1.05 2.21'104 CO2 3340 241.5 From these results, it can be concluded that said combination of aqueous CuSO4 wash and amine wash removes H2S and CO2 effectively.
Table 3. Energy consumption as steam and electricity used for the absorption steps.
Wash LP steam Electricity (MW) (MW) Me0H 46 26 CuSat+Amine 30 7 These results confirm the effect of the present method for both the steam and electricity consumption. It verifies the energy efficiency of the removal of sulfur components and carbon dioxide from the syngas.

Claims (12)

Claims

1. A method for washing hydrogen sulfide and carbon dioxide from a gas obtainable by gasification of carbonaceous biomass, said method comprising a. contacting said gas with a first absorbent solution comprising transition metal ions, said transition metals selected from copper, zinc, iron and cobalt and mixtures thereof, in acidic aqueous solution;
b. binding hydrogen sulfide to said first absorbent solution;
c. recovering the gas from step b;
d. contacting recovered gas from step c with a second absorbent solution comprising an alkaline absorbent;
e. binding carbon dioxide to said second absorbent solution;
f. recovering the washed gas from step e.

2. The method according to claim 1, wherein the concentration of the transition metal ion in the wash solution is less than about 1000 ppm w, and preferably less than about 100 ppm w, calculated from the weight of the first absorbent solution.

3. The method according to claim 1 or 2, wherein said transition metal ions comprise copper, preferably as CuSO4.

4. The method according to claim 1 wherein the contacting of said gas with a first absorbent solution takes place at a temperature from 10 to 80 °C and at a pressure from 1 to 50 bar.

5. The method according to claim 1 wherein the contacting of said gas with a second absorbent solution takes place at a temperature from 10 to 80 °C, preferably from 20 to 40 °C.

6. The method according to claim 1, 4 or 5 wherein the contacting of said gas with a second absorbent solution takes place at substantially the same temperature and/or same pressure as said contacting of the gas with the first absorbent solution.

7. The method according to any one of the preceding claims wherein the H2S
level of the gas recovered from step f is less than 20 ppb, preferably less than 1 ppb.

8. The method according to claim 1, wherein said first and/or second absorbent solution is/are regenerated after gas recovery.

9. A method for producing hydrocarbons or derivatives thereof from biomass raw material comprising the steps:
i. gasifying the biomass raw material in the presence of oxygen to produce a gas comprising carbon monoxide, carbon dioxide, hydrogen, water and hydrocarbons;
ii. optionally a tar reforming step iii. optionally removing tar components from the gas;
iv. optionally adjusting the hydrogen to carbon monoxide ratio;
v. wash according to claim 1;
vi. converting in a synthesis reactor at least a significant part of the carbon monoxide and hydrogen contained in the gas into a product selected from hydrocarbon composition and derivatives thereof; and vii. recovering the hydrocarbon or derivative thereof as the product.

10. The method according to claim 9, wherein step v is preceded by a COS
hydrolysis step.

11. The method according to any one of the preceding claims, wherein said alkaline absorbent is selected from amines, carbonates, aqueous CaO solution and combinations thereof.

12. The method according to any one of the preceding claims, wherein said second absorbent solution is applied as an aqueous amine wash, carbonate wash, carbonate precipitation or a combination thereof.